Method of the synthesis of ammonia from the nitrogen and hydrogen mixture produced from the natural gas

FIELD: petrochemical industry; methods of the synthesis of ammonia from the nitrogen and hydrogen mixture produced from the natural gases.

SUBSTANCE: the invention is pertaining to the field of petrochemical industry, in particular, to the method of the synthesis of ammonia from the nitrogen and hydrogen mixture produced from the natural gases. The method of the catalytic synthesis of ammonia from the mixture of nitrogen and hydrogen provides, that the natural gas together with the oxygen-enriched gas containing at least 70 % of oxygen is subjected to the autothermal reforming at temperature from 900 up to 1200°C and the pressure from 40 up to 100 bar at the presence of the catalyzer of cracking, producing the unstripped synthesis gas containing in terms of the dry state 55-75 vol.% of H2, 15-30 vol.% of C and 5-30 vol.% CO2. At that the volumetric ratio of H2: CO makes from 1.6 : 1 up to 4 : 1. The unstripped synthesis gas is removed from the furnace of the autothermal reforming, cooled and subjected to the catalytic conversion producing the converted synthesis gas containing in terms of the dry state at least 55 vol.% of H2 and no more than 8 vol.% of CO. The converted synthesis gas is subjected to the multistage treatment for extraction ofCO2, CO and CH4. At that they realize the contact of the synthesis gas with the liquid nitrogen and using at least one stage of the absorption treatment produce the mixture of nitrogen and hydrogen, which is routed to the catalytic synthesizing of ammonia. At that at least a part of the synthesized ammonia may be transformed into carbamide by interaction with carbon dioxide. The realization of the method allows to solve the problem of the ammonia synthesis efficiency.

EFFECT: the invention ensures solution of the problem of the ammonia synthesis efficiency.

8 cl, 1 ex, 2 tbl, 2 dwg

 

The invention relates to a method for catalytic synthesis of ammonia from nitrogen and hydrogen.

From German patent application DE 2007441 know about obtaining ammonia from synthesis gas, and by gasification of hydrocarbons receive raw synthesis gas, which bassereau, convert, free from carbon dioxide and, finally, subjected to washing with liquid nitrogen to remove residual impurities. In European patent application EP 0307983 describes a similar way, and the converted synthesis gas before receiving ammonia is subjected to washing with liquid nitrogen. A detailed description of the catalytic synthesis of ammonia is contained in Ullmann''s Encyclopedia of Industrial Chemistry, 5. Edition, Band A2, Seiten 143-215. In the same publication (Band A27, Seiten 333-350) describes the obtaining of urea. A combined method for the synthesis of ammonia and urea is described in European patent application EP-A-0905127.

The present of the invention is possible to increase the efficiency of the synthesis of ammonia and to provide a method suitable for practical use, including large industrial installations. According to the invention this problem is solved by the fact that natural gas together with oxygen-rich gas is sent into the oven for autothermal reforming, in which at a temperature of from 900 to 1200°C and a pressure of from 40 to 100 bar in outstay catalyst cracking receive raw synthesis gas, contains 55-75% vol. H2, 15-30 vol.% CO and 5-30 vol.% CO2in terms of dry condition, and the volume ratio of H2:CO range from 1.6:1 to 4:1; crude synthesis gas is removed from the oven for autothermal reforming, cooled and subjected to catalytic conversion to convert CO in H2receiving the converted synthesis gas containing at least 55% vol. H2and not more than 8% vol. CO in terms of dry condition; converted synthesis gas is subjected to multi-stage purification to extract CO2, CO and CH4; get a mixture of N2+H2that referred to the catalytic synthesis of ammonia.

An important feature of the method according to the invention is opt to obtain a crude synthesis gas plants designed for the conversion of natural gas with steam (steam reforming). Autothermal reforming can be carried out at relatively high pressure of from 30 to 100 bar, mostly from 40 to 80 bar. High pressure discharged from the kiln for reforming gas flow can be preserved almost unchanged, and therefore before applying the synthesis gas in a synthesis system for ammonia it should be subjected to only a slight compression. Thanks to this method according to the invention has a much higher economic the spine compared with traditional ways of reforming of natural gas with water vapor, according to which it is allowed to use only relatively low pressure. Another advantage of autothermal reforming of natural gas compared to its conversion in the presence of water vapor is in the formation of synthesis gas, which is characterized by such a value of H2:CO2in which the quantity of carbon dioxide emitted by absorption purification converted gas is sufficient to result in urea only synthesized ammonia.

The preferred embodiment of the invention is that the interaction with carbon dioxide to obtain urea is subjected to at least a portion of the synthesized ammonia. This is preferred if the carbon dioxide is extracted from the converted synthesis gas using at least one stage absorption purification, and carbon dioxide is used to produce urea. One of several possibilities for the implementation of this technology provides the use described in European patent application EP-A-0905127 combined method. Unlike traditional methods, the amount of carbon dioxide that contribute to absorption stage purification of synthesis gas, usually is enough to meet the needs dioxide required for the sushestvennee synthesis of urea.

Carbon dioxide may preferably be extracted from the converted gas mixture by physical washing carried out, for example, methanol, at temperatures from -20 to -70°C. When this consumes a relatively small amount of energy, including the energy of compression. Through the regeneration of the washing liquid can be distinguished, at least half of the carbon dioxide under pressure, for example, from 2 to 8 bar, so that subsequent use of the separated carbon dioxide for the synthesis of urea saved spent on compression energy.

It is expedient, if the oxygen-enriched gas stream supplied to the furnace for autothermal reforming, contains at least 70 vol.%, mostly, at least 90 vol.% oxygen, reducing the amount present in the raw syngas impurities and can be simplified absorbent cleaning.

Possible embodiments of the method according to the invention is represented by the following schema.

Figure 1 shows flow chart of the method.

Figure 2 shows the technological scheme of the alternative method.

In accordance with Figure 1 in which is designed for preparing the raw materials unit (40) via the pipeline (1) direct natural gas and pipeline (a) water vapor for the implementation of the usual preparatory process operations: desulfurization, heating and removal of C2+-components. In addition, the unit (40) via the pipeline (42) serves containing methane gas. Consisting mainly of methane and water vapor mixture in pipe (43) is fed to the burner (2) oven for autothermal reformer (3). At the same time in the burner (2) on the pipe (4) with installation for air separation (5) direct the oxygen-enriched gas, the oxygen content which is usually at least 70 vol.%, preferably, at least 95 vol.%. Into the oven for reforming (3) in the form of a stationary layer (For) put one of the known granular cracking catalysts, such as catalyst based on Nickel. The pressure in the furnace (3) is from 30 to 100 bar, preferably from 40 to 80 bar temperature from 900 to 1200°C. Remove from the oven (3) through a pipeline (7) crude synthesis gas contains 55-75% vol. H2, 15-30 vol.% CO and 5-30 vol.% CO2moreover , the volume ratio of H2:CO is from 1.8:1 to 4:1. After cooling in the heat exchanger (8) raw synthesis gas by pipeline (9) is directed to the catalytic conversion of (10), which may consist of several reactors. Catalytic conversion is carried out at a temperature of from 150 to 500°C, preferably at a temperature of from 280 to 450°C, using well-known designed for this purpose, the catalysts, for example, produce the p on the basis of iron. By catalytic conversion of CO+H2O turn in CO2+H2. The preferred volume ratio of H2:CO2exhaust pipeline (11) of the converted gas is from 2.5:1 to 3:1 (calculated on the dry state).

The converted synthesis gas is discharged from the installation (10) through a pipeline (11)contains at least 55%, preferably, at least 65% hydrogen in terms of dry condition and not more than 8% vol. CO. The converted synthesis gas is subjected to the heat exchanger (12) indirect cooling, after which the pipe (13) is directed to the installation of an absorption treatment (14), in particular, for the recovery of carbon dioxide. Absorption treatment can be carried out, for example, by physically cleaning the synthesis gas methanol at a temperature of from -70 to -20°C. in Addition, for washing the synthesis gas can be used, and other solvents such as methyldiethylamine or selecsol (Selexol). Containing carbon dioxide wash solution through the pipeline (16) is directed to the installation for regeneration (17), where they perform desorption dioxide. The regenerated wash solution through the pipeline (18) return to the setup absorption treatment (14). Allocated in this way carbon dioxide in quality is quite suitable for the synthesis of urea on the mount (21), on odorou it is served by pipeline (20).

Partially cleared for the installation of an absorption treatment (14) synthesis gas by pipeline (22) is directed to the second installation of the absorption treatment (23), where the drilling fluid used liquid nitrogen. Required for washing the synthesis gas nitrogen enters with installation for air separation (5) through the pipeline (6). Details regarding absorption purification designed to produce ammonia synthesis gas with liquid nitrogen, contained in the above European patent EP 0307983. Usually, installing the absorption treatment (23) are obtained containing carbon monoxide gas by pipeline (41) returns to the catalytic conversion (10). If both get enriched with methane gas, by pipeline (42) it is sent for the processing plant raw material (40). To contribute to the production of cold by pipeline (1b) for the installation of (23) serves natural gas, under pressure from 10 to 100 bar, preferably under pressure, comprising at least 30 bar. Natural gas on the installation of an absorption treatment (23) drossellied so that its pressure decreased, at least up to 8 bar, preferably at least 2.5 bar. Throttled natural gas similar to methane pipeline (42) can be directed, for example, to install (40).

Absorbsion the second gas cleaning installation (23) carry out so, so that the molar ratio of H2:N2exhaust pipeline (24) the synthesis gas was approximately 3:1. The washed liquid nitrogen synthesis gas by indirect heat exchange heat in the heat exchanger (45), and then compressed in the compressor (46) and the pipeline (24A) is directed to the installation of the ammonia synthesis, which includes the reactor (25) with indirect cooling and operated in an adiabatic mode, the reactor (26). The mixture formed recirculating pipeline (27) synthesis gas and sent by pipeline (24A) fresh synthesis gas, the temperature of which is from 100 to 200°C, sent by pipeline (27A) in the tube (28) or the channels of the reactor (25), and the function of the cooling medium, intended for removal of heat of reaction from the catalyst (25A), performs the synthesis gas. Alternatively, a cooling medium to remove heat generated during the synthesis of ammonia, can serve as boiling water.

Coming out of the reactor (25) synthesis gas, whose temperature is from 300 to 500°C, the pipe (29) is sent to the reactor (26), where it is in contact with a stationary catalyst bed. The synthesis of ammonia is exothermic effect, so the reaction mixture, the temperature of which ranges from 400 to 600°C, the pipe (30) is directed to a refrigerator (31). Ammonia synthesis gas p is the pipe (32) is sent to the reactor (25) for indirect cooling in it stationary catalyst layer. The temperature of the gas in the pipe (33) at the outlet of the reactor (25) is from 300 to 500°C, preferably from 380 to 430°C. the Concentration of ammonia in the reaction mixture discharged by the pipe (33)is at least 20 vol.%, and in addition to ammonia mixture mainly contains nitrogen and hydrogen. The reaction mixture is cooled in a multi-stage refrigerator (34) and sent to a separator (35). Liquid crude ammonia from the separator (35) is drained through line (36). Gaseous components return from the separator (35) through the pipeline (27) into the reactor (25) as the recirculating gas.

Crude ammonia can be fully or partially removed from the installation synthesis pipeline (37) and is aimed for use in these or other known purposes. In addition, crude ammonia can be fully or partially directed by pipeline (38) for the installation of the synthesis of urea (21), which is carried out in a known manner. The resulting urea display with installation (21) through the pipeline (39).

As shown in Figure 2 process flow generated at the facility for catalytic conversion (10) synthesis gas by pipeline (11) is sent to the heat exchanger (12), then it is compressed using the compressor (15), and further along the pipe (13) is sent to the absorber (14a) to extract carbon dioxide is a weak solution of carbamate entering the installation of the synthesis of urea (21) through the pipeline (18). Containing carbon dioxide wash solution through the pipeline (16) return on the installation of the synthesis of urea (21). Partially purified synthesis gas by pipeline (22) is directed to the installation of thin clearing (23a), which may be implemented, for example, by washing with liquid nitrogen, adsorption by variable pressure or the conversion of carbon dioxide to methane. The supply of natural gas by pipeline (I) suitable only when washing the synthesis gas with liquid nitrogen.

Ammonia is synthesized by a method similar to that described in the review is shown in figure 1 flowsheet. The reaction mixture from the refrigerator (34) on the pipe (33a) is fed to the absorber (35A), where the ammonia is washed supplied by pipeline (50) water. Ammonia water pipe (51) is directed to the installation of the synthesis of urea. Detailed description of the synthesis of ammonia is described in European patent application EP-A-0905127. Other digital designations indicated in figure 2, similar to that shown in figure 1.

The method of synthesis of ammonia according to the invention compared with the known methods has, in particular, the following advantages:

1. Excluded conversion of natural gas with steam (steam reforming), which means the rejection of the use of bulky and expensive equipment. At the same time it enables the set created more preferable conditions for the cracking of methane and other hydrocarbons at high pressure compared to the conversion of water vapor.

2. The nitrogen in the mixture of N2+H2preferably introduced only at the stage of washing the synthesis gas with liquid nitrogen. The necessity of its introduction in the earlier process stages of obtaining and purification of hydrogen is absent.

3. More appropriate is the production of methane when washing the synthesis gas with liquid nitrogen and its recirculation into the oven for autothermal reforming. Due to this, the reforming can be carried out at extremely low temperatures of about 950°C, and there is no need to ensure the absence of methane in the gas mixture leaving the furnace. In addition, it is possible throttling of natural gas supplied to the plant for washing the synthesis gas with liquid nitrogen under pressure of from 10 to 100 bar, for the production of cold (Joule-Thompson).

4. More appropriate is to obtain when washing the synthesis gas with liquid nitrogen gas stream enriched in carbon monoxide, which return to the stage catalytic conversion. Thanks to the presence of residual carbon monoxide in the converted gas mixture should not be construed as a violation of technology: its content in the converted synthesis gas can reach 8%, mostly not exceeding 4%. Thanks to the implementation of the catalytic con the version you use is reliable in operation and economical catalysts based on iron and refuse more sensitive catalysts based on copper.

5. Gas cleaning by washing with liquid nitrogen results in a mixture of N2+H2possessing a high degree of purity, and therefore it is possible to completely abandon the removal of part of the recirculating gas or to remove only a small amount.

6. The amount of waste heat is enough to offset the need for energy, including the energy needed to compress the synthesis gas directed to the obtaining of ammonia and the subsequent synthesis of urea.

7. Consumption of natural gas for ammonia synthesis (taking into account the lower limit calorific value) does not exceed 27,3 kJ/t, and the synthesis of urea is not more than 19 kJ/t, that is much lower in comparison with known methods. These consumable parameters form the basis of the following example.

8. Technological equipment for implementing the method according to the invention, may be composed of individual modules, and for its installation requires a relatively small area.

Example

Method implemented in accordance with the presented figure 1 is a flow diagram, with a daily capacity can be 3000 tons of ammonia or 5263 tons of urea. The part below the data obtained by calculation.

Pipeline (1) serves natural gas pipeline (1A) is tanoy pairs, moreover, the molar ratio of water vapor to hydrocarbon is to 2.55:1. Table 1 shows the expenditure parameters, temperature, pressure and composition of gas mixtures (in vol%).



Table 1
Digital signs14371124A27A3320
Flow rate (t/h)92263336357127382382162
Temperature (°C)2565953216817540332
Pressure (bar)556160571371431403
The composition of CH4for 91.327,01,82,0---0,8
C2H45,8-------
CO-1,610,61,1---
CO21,90,67,116,7---99,0
Argon--0,30,5---0,1
H2-3,238,747,574,870,854,10,1
N21,00,30,42,325,224,418,9-
H2O-67,341,129,9----
NH3-----4,827,0-

The oxygen content in the send pipeline (4) gas is 95%. The synthesis gas in the pipe (24) contains less than 5 ppm (vol.) of carbon monoxide and about 25 parts per million (vol.) argon. The catalyst (3A) on the basis of Nickel oxide (NiO), as well as catalysts for the synthesis of ammonia are standard products manufactured in cast the STI, firm Süd-Chemie (Munich (DE), type G-90, AS-4). The temperature at the inlet to the furnace for reforming (3) is 950°C. At this temperature, total gas consumption is minimal.

Catalytic conversion (10) carry out, passing the synthesis gas through gas-cooled reactor with similar reactor (25) design. Next, the reaction mixture is passed through the intermediate fridge and operated in an adiabatic mode, the reactor with a fixed bed of catalyst. The conversion is carried out, using manufactured by Süd-Chemie standard gelatobaby catalyst type G-3C. The residual content of carbon monoxide in the converted synthesis gas does not exceed 1.6% (in terms of dry state), the volumetric ratio of H2:CO2=2,84 (in terms of dry state).

Absorption gas cleaning (14, 17) provide a way for rectisol (Rectisol-Verfahren), removing carbon dioxide with methanol at a temperature of -58°C. the installation for gas washing liquid nitrogen (23) the synthesis gas is first cooled to a temperature of -185°C. Cooling is accompanied by condensation of methane, which is isolated and removed by pipeline (42). Then in the contacting gas with liquid nitrogen is the condensation of carbon monoxide, which is isolated and the pipe (41) is directed to kataliticheski the Yu conversion. Table 2 shows the composition of the gas streams (in%vol.) in pipelines (41) and (42).

Table 2
(41)(42)
CH45,1352,54
CO21,1812,27
CO2-0,53
Argon7,188,64
H29,766,75
N256,7519,27

Due to the heat exchange of the gas mixture in the cooling system (34) with cooling water condensation occurs 65% of the ammonia. Part of the gas flow (purge gas purge gas) is separated from the recycle gas in order to remove impurities.

1. Method for catalytic synthesis of ammonia from nitrogen and hydrogen, characterized in that the natural gas together with oxygen-rich gas containing at least 70 vol.% oxygen is subjected to the autothermal reformer at a temperature of from 900 to 1200°C and a pressure of from 40 to 100 bar in the presence of a catalyst cracking unit, receiving the crude synthesis gas containing, calculated on the dry state 55-75% vol. H2, 15-30 vol.% CO and 5-30 vol.% CO2moreover , the volumetric ratio of H2:CO with the hat from 1.6:1 to 4:1, the crude synthesis gas is removed from the oven for autothermal reforming, cooled and subjected to catalytic conversion, receiving the converted synthesis gas containing, calculated on the dry state at least 55% vol. H2and not more than 8% vol. CO converted synthesis gas is subjected to multi-stage purification to extract CO2, CO and CH4and carry out the contacting synthesis gas with liquid nitrogen, using at least one stage absorption treatment, receive a mixture of nitrogen and hydrogen, which is directed to the catalytic synthesis of ammonia.

2. The method according to claim 1, characterized in that at least part of the synthesized ammonia is converted into urea by reacting with carbon dioxide.

3. The method according to claim 1 or 2, characterized in that from the converted synthesis gas is extracted CO2using at least one degree of absorption and cleaning, and at least part of the extracted CO2direct the synthesis of urea.

4. The method according to claim 1 or 2, characterized in that CO2from the converted synthesis gas is extracted by physical washing with methanol at a temperature of from -70 to -20°C.

5. The method according to claim 1 or 2, characterized in that by absorption of cleaning liquid nitrogen from the synthesis gas extract containing CO gas, which is directed to the catalytic CONV is rsiu.

6. The method according to claim 1 or 2, characterized in that the mixture of nitrogen and hydrogen is sent to the stage of synthesis of ammonia in a reactor containing at least two of the catalyst, and this mixture serves as a cooling medium for indirect cooling located in one of the reactors of the catalyst.

7. The method according to claim 1 or 2, characterized in that the volume ratio of H2:CO2in formed during the conversion of the synthesis gas is from 2.5:1 to 3.0:1, calculated on the dry state.

8. The method according to claim 1 or 2, characterized in that the stage of absorption and purification of the synthesis gas with liquid nitrogen send natural gas under pressure from 10 to 100 bar, through its throttling up to 8 bar.



 

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4 tbl, 4 ex

FIELD: chemical industry; methods of realization of the chemical transformations by compression of the gas-containing mixtures.

SUBSTANCE: the invention is pertaining to the chemical technology and may be used in chemical industry for realization of the different chemical transformations, for example, for the air nitrogen fixation or for production of the synthesis gas. The method of realization of the chemical transformations by compression of the gas-containing mixtures includes the two-stage superadiabatic compression of the reaction mixture in two successive strokes by the piston in the cylinder of the superadiabatic compression reactor divided into the main and additional chambers the transversal septum made with a possibility of the mixture bypassing. The second stage of the superadiabatic compression on each stroke is realized simultaneously with the bypassing of the reaction mixture into the additional chamber of the cylinder. At that the compression power is kept equal on the first and the second compression strokes by selection of the value of the relative volume of the additional chamber of the cylinder β = V2/(V1 + V2), where V1 is the volume of the main chamber, V2 is the volume of the additional chamber, which for the pressure of up to 300 atm should be of no less than 0.01, and the injection of the reaction mixture into the reactor is performed before the first stroke of the two-stage compression at the piston motion to the lower dead point. The simultaneous bypassing and compression of the mixture at the second stage of the superadiabatic compression on each stroke is performed at constant pressure. Before or in the beginning of the second compression stroke the component consisting out of the polyatomic molecules is introduced. At realization of the exothermal chemical transformations the heat-accumulating component with the developed surface is mounted in the additional chamber of the cylinder. The invention ensures the reliable and high-effective running of the chemical reactions.

EFFECT: the invention ensures the reliable and high-effective running of the chemical reactions.

4 cl, 1 dwg

FIELD: heat power generator operation methods comprising direct action of combustion products upon heated medium, possibly generation of heat power and supplying it through heat transfer agent to user.

SUBSTANCE: method comprises plasma-electrolytic action upon liquid for producing steam, hydrogen and oxygen. Said plasma-electrolytic action upon liquid (water) is realized in capillary-porous hydrophilic material. Then hydrogen is oxidized by means of oxygen in atmosphere of generated steam to which are added liquid and (or) gas phases whose quantity provides regulation of mixture temperature. Water-adsorbing matter is used in said capillary-porous hydrophilic material. Added phase is ejected by means of generated hydrogen, oxygen and steam; water is used as added liquid phase and inert gas is used as added gas phase.

EFFECT: lowered power consumption, weakened aggressive action of heat transfer agent upon materials of heat power generator.

5 cl, 1 dwg, 1 ex

FIELD: chemical industry; reactor.

SUBSTANCE: the invention is pertaining to reactor. The method includes preparation of suspension of the finely dispersive powdery aluminum in water, creation in the reactor of pressure of the saturated water steams, sputtering of the suspension into the high-pressure reactor, withdrawal from the reactor of the mixture of the steams and hydrogen, and also withdrawal from the reactor of aluminum hydroxide or aluminum oxide into the receiving device, measuring of the temperature in the reactor, measuring of the gas mixture pressure in the reactor. Determine the partial pressure of the saturated water steam in the reactor, determine the partial pressure of hydrogen, determine the free volume of the reactor and, changing the mass of aluminum being introduced in the composition of the suspension according to the formula make adjustment of the pressure and temperatures in the reactor. The device contains: the source of the suspension of the finely-dispersed powdery aluminum with water and the mixer, the reactor, the condenser, the receiving device, the adjustable valve of the mixture withdrawal of the mixture of the water steams and hydrogen, the adjustable valve of withdrawal of aluminum hydroxides or oxides, the sensor of the reactor temperature, the sensor of pressure on the inlet of the suspension delivery into the reactor, the sensor of pressure on the outlet of the steam-gas mixture, and the sensor of pressure in front of the inlet of the steam- gas mixture into the condenser, the adjustable tool of the suspension delivery into the reactor, the main control unit with the inlet and the outlet. At that the source of suspension contains the adjustable tool of the water delivery and the adjustable tool of delivery of the aluminum powder. The invention allows to improve stability of the reactor operation.

EFFECT: the invention ensures the improved stability of the reactor operation.

5 cl, 3 dwg, 1 tbl

FIELD: hydrocarbon conversion catalysts.

SUBSTANCE: catalyst for generation of synthesis gas via catalytic conversion of hydrocarbons is a complex composite composed of ceramic matrix and, dispersed throughout the matrix, coarse particles of a material and their aggregates in amounts from 0.5 to 70% by weight. Catalyst comprises system of parallel and/or crossing channels. Dispersed material is selected from rare-earth and transition metal oxides, and mixtures thereof, metals and alloys thereof, period 4 metal carbides, and mixtures thereof, which differ from the matrix in what concerns both composition and structure. Preparation procedure comprises providing homogenous mass containing caking-able ceramic matrix material and material to be dispersed, appropriately shaping the mass, and heat treatment. Material to be dispersed are powders containing metallic aluminum. Homogenous mass is used for impregnation of fibrous and/or woven materials forming on caking system of parallel and/or perpendicularly crossing channels. Before heat treatment, shaped mass is preliminarily treated under hydrothermal conditions.

EFFECT: increased resistance of catalyst to thermal impacts with sufficiently high specific surface and activity retained.

4 cl, 1 tbl, 8 ex

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